JP3548573B2 - Combined plant with combustion and exhaust gas filter - Google Patents
Combined plant with combustion and exhaust gas filter Download PDFInfo
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- 238000002485 combustion reaction Methods 0.000 title claims description 41
- 239000007789 gas Substances 0.000 claims description 44
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 16
- 239000001301 oxygen Substances 0.000 claims description 16
- 229910052760 oxygen Inorganic materials 0.000 claims description 16
- 238000000926 separation method Methods 0.000 claims description 13
- 239000000126 substance Substances 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 239000000356 contaminant Substances 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 3
- 238000001704 evaporation Methods 0.000 claims description 2
- 230000008020 evaporation Effects 0.000 claims description 2
- 239000000446 fuel Substances 0.000 claims 1
- 230000003116 impacting effect Effects 0.000 claims 1
- 239000007788 liquid Substances 0.000 claims 1
- 239000000203 mixture Substances 0.000 claims 1
- 239000007787 solid Substances 0.000 claims 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 28
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 24
- 229910002092 carbon dioxide Inorganic materials 0.000 description 14
- 239000001569 carbon dioxide Substances 0.000 description 14
- 229910052757 nitrogen Inorganic materials 0.000 description 12
- 238000001914 filtration Methods 0.000 description 9
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 8
- 238000000034 method Methods 0.000 description 6
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 5
- 239000003344 environmental pollutant Substances 0.000 description 5
- 231100000719 pollutant Toxicity 0.000 description 5
- 238000004064 recycling Methods 0.000 description 4
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 229910001882 dioxygen Inorganic materials 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000383 hazardous chemical Substances 0.000 description 1
- 238000005338 heat storage Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0045—Vacuum condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
- F02C3/36—Open cycles
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/32—Direct CO2 mitigation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Analytical Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Treating Waste Gases (AREA)
- Air Supply (AREA)
- Chimneys And Flues (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
本発明は請求の範囲第１項の記載部分に対応する一種の燃焼及び排気ガス濾過プラントの組合せに関するものである。
このようなプラントは既知であり、実際に十分の性能を有している。濾過は、非常に高度化に行うことができ、かつこの種のプラントではスペースをほとんど必要とせず、それは、利用されているプラントを改変する際に重要なことである。このためのすべての工程段階は、濾過工程それ自体に集中されてきた。しかしながら、このようなシステムは、燃焼装置と膨張ガス濾過プラントとの整合性をより良くすることによって一層向上させることが可能なことがわかっている。
したがって、本発明の目的は、燃焼及び排気ガス濾過プラントの組合せための濾過効果及びスペース条件を一層の向上させることである。
本発明によれば、始めに上記の種類の燃焼及び排気ガス濾過プラントの組合せにおける燃焼室を酸素ガス100％まで引き上げた燃焼用空気を供給する装置に接続し、そして分離装置を、最終膨張工程後に分離装置内に蓄積した少量の非凝縮ガスをポンピングによる処理のための真空ポンプまたはその類似物に接続することにより、このことは達成される。
事実、燃焼用空気は窒素４部と酸素１部、それに少量の他の物質を含んでいる。燃焼は酸素の量が十分であることが必要であるが、これに対し、窒素は燃焼を妨げるのみである。一方で窒素は燃焼中かなりの量の危険物質を発生し、また一方でガス質量は非常に増大する。窒素３部に対して酸素が２部まですでに増加したものは燃焼必要空気を半分まで減少させる。純粋な酸素であれば、圧縮機の効果は80％以下に減る。燃焼空気の体積が甚だしく減少すると、基本的に燃焼室の大きさは限定される。燃焼室の温度は、同量のエネルギが燃焼中解放されるので、上昇する。この温度上昇は、より熱蓄積面積を大きくし、熱輻射を増加させることによって、平衡を保つができる。
しかしながら、窒素の含有量はおそらく燃焼室内で減少し、非常に純度の高い排気ガスが得られるので、排気ガス濾過側に最も大きな進歩をもたらす。また、窒素が含まれると、多様な種類の酸化窒素が燃焼中に発生し、これらを分離するのは非常に困難である。純粋な酸素が燃焼している間は、高い燃焼温度が得られるか否かに拘らず、酸化窒素は発生しない。酸素リッチの雰囲気においては、水溶性酸化物N2及びN2O5が最初に発生し、これらは比較的分離し易い。
排気ガスは、N2,CO2,H2O及び少量の酸化窒素と燃焼中に含まれていた汚染物質とから成る。水蒸気の一部が、水と共に洗浄装置の中で凝縮し、NO2とN2O5がSO3及びCLタイプその他の物質などを含む汚染物質の大部分と同様にその中に溶解する。洗浄装置の後では、N2,CO2及び少量の物質は水溶性ではなく、また洗浄装置のすぐ後方の温度で凝縮される。燃焼用空気が酸素を多く含めば含むほど、それだけ膨張室のすぐ前方の排気管ガスの中の窒素の量は少なくなる。当然、酸化窒素及び他の汚染物質の量は別の化学物質を洗浄水に添加することにより相補物（complement）として減らすことができる。
膨張装置において、温度は流入ガス温度と圧力降下によって決定されるレベルまで低下する。最終温度が−50℃以下であれば、排気ガス中の汚染物質はガス中の水蒸気と共に凝縮する。温度が−120℃以下に降下する時、すべての二酸化炭素も凝縮してしまう。膨張室における圧力降下が１つ工程で発生するなら、氷結した雪と二酸化炭素の雪が汚染物質を含むことになる。したがって、雪と汚染物質を凝縮する工程と純粋な二酸化炭素を凝縮する工程との２つ工程で膨張を行うと便利である。
この装置により、水、二酸化炭素及び排気ガス中のすべての汚染物質は可能な限り排除される。含まれる窒素と不活性ガスが残るのみである。仮に酸素だけが使用された場合、ほとんどすべてのガスが凝縮物に転化されてしまい、凝縮物を連続的に送出し、さらに分離室を外の大気に対して閉鎖した状態に保つことにより、最終圧力は０バールに近く保つことができる。この低い圧力は膨張室または膨張室のうちの最後の一つにおける圧力降下を増大させ、その効率を大きく向上させる。また、その効率は100％以下の酸素含有量の場合に向上するが、極限までになることはない。この低い圧力を維持するために、真空ポンプが使用され、分離装置からの残留ガスを連続的に吸引する。
第一膨張ユニット以前の温度が低いと、膨張装置以降の温度は降下する。二酸化炭素の雪を洗浄装置にリサイクルすることにより、一方では膨張前により良い冷却が得られ、他方では、かなり大きなガス流れが膨張装置を介し得られる。直線的熱力学的条件において、元々の考えのガス・タービン・システムは、機械的エネルギの供給を必要とし、出口温度は入口温度よりも低い。しかしながら、そのプロセスは、上記の方法で凝縮した二酸化炭素をリサイクルし、かつこの装置でシステム内のバランスを達成することによって変化する。すなわち膨張は圧縮が必要とするのと同じだけのエネルギを発生することができる。二酸化炭素をより多くリサイクルさせることにより、膨張装置は圧縮機の要求以上の機械エネルギを発生する。このような方法で、熱エネルギは機械エネルギに変換することができる。たくさんの凝縮二酸化炭素をリサイクルすることにより、最大の転化を達成することができ、その蒸発熱は燃焼中に供給されるエネルギに、またはシステムに関連する。実施例においては、また、膨張装置の温度が０℃よりも高いことが維持されるべきである。また、例えば膨張室に０℃より高い温度を持つ水の形態で外部から熱エネルギを供給することが可能である。その後このエネルギは機械エネルギに変換される。
一例として、圧力は膨張工程間で圧縮機、または熱交換器でガスを加熱することにより、増大させることができる。また、排気ガス中の窒素の量を制限すると、圧縮されるべきガスの量を制限することができる。
膨張工程間のガスを冷却することにより、簡便に膨張後に発生する冷いガスによって最終温度がより低くなるか、またはより低い初期圧力で最終温度を得ることができる。従って圧縮効果を小さくすることができる。
流入する燃焼用空気における窒素の量を制限するための最も簡単な方法は、酸素ガスボンベから必要な酸素を供給することである。より大きなプラントにおいて、経済性をより向上させるには、例えばガス分離膜の使用をすることである。それから発生する酸素は燃焼プラント内で使用され、これに対し加圧された窒素は発電機を駆動することができ、または別の用途のために加圧されたまま蓄積することができる。膜技術や他の分離方法は急速な発展を示しており、例えば水から酸素を生産するようにある程度純粋な酸素を得るための方法は重要である。
上記の種類のプラントからの排気ガスは始動中に圧縮機によって燃焼室へリサイクルすることができる。排気ガスはすべての環境影響物質を排除し、おそらく流入する燃焼用空気よりきれいである。
酸素を発生するために必要な電気エネルギ及び必要な圧縮機やポンプはそれぞれ、上記の装置を備えたプラントにおいて利用されている。プラントの駆動における低温は低温を必要とする他の工程のために使用することができる。
本発明によるプラントは、熱力または電力プラントとの組み合わせで使用される種々の方法によって変更することができ、燃焼エンジンは、この方法により高効率で開発させることができ、二酸化炭素さえも含まない完全に純粋な排気ガスを送出する。
本発明は本発明による燃焼及び排ガス濾過プラントの組合せを例を上げ、概略的を示した添付図面を参照しながら以下に詳細に説明する。
図はモータ１により駆動され、酸素／窒素分離膜３に接続される圧縮機２を示し、その膜の酸素側はさらに圧縮機４を経由して燃焼室５に接続されている。その室５には例えばオイル用バーナー７を有する燃焼供給ライン６が導かれている。さらに、環境影響物質を含む物質は、燃焼室５で燃焼させるために（図示しないが適した方法で）燃焼室５内に供給され得る。おそらくはまた、酸素を含むボンベ８は、必要ならば酸素含有量を増加させるために燃焼室５に接続することができる。
排気ガスは、洗浄及びさらに加圧された冷却のためにスクラバ12へ供給される少し前に排気ガス温度を低下させるボイラ／クーラ10に接続されるライン９を経由して燃焼室５を離れる。排気ガス中の水蒸気の一部はここで凝縮する。粒子状で水溶性形態であり、かつその後で既知の方法で加圧されたスクラバから導出される汚染物質を処理するため、凝縮物は、スクラバ内の洗浄水と共に使用される。残りの汚染物質を含む排気ガスは、スクラバから、例えば発電機15を駆動するのに適当である回転スクリュー式の第一膨張機14へライン13を経由して送給される。膨張機を経由して高速の圧力減少が行われ、同時に膨張機を通過し、排気ガスの温度は約−50℃まで低下させ、その後出力装置17により減らすことのできる多くの汚染物質を含む、例えば氷結した凝縮物の形態で、第一分離室16内に送給される。残りの排気ガスは発電機19を駆動する第二膨張機20へライン18を経由して送給され、ここで排気ガスは、主に二酸化炭素から成る残りの排気ガスを凝縮させるような方法で、さらに急速な圧力減少とそれに伴う約−120℃の温度低下状態にさらされ、その後凝縮物はライン21を経由して膨張機20と接続する出力ライン23を備えた第二分離室22から出力される。ポンプ25を備えるもう一つの出力ライン24が、二酸化炭素凝縮物を二酸化炭素に蒸発し、それを再膨張し、スクラバ12にリサイクルするために適用される。高度に濾過される残留廃棄ガスは第二分離室22内である程度の真空を維持する真空ポンプ27を備えた出力ライン26から第二分離室22を離れる。
ライン24内の低温である二酸化炭素は、配置され得る回転スクリュー式の第二の、または追加の膨張機への入力のための再冷却にも使用することができる。同様に、圧縮機が設置され得、その結果、配置され得る第二の膨張機及び追加の膨張機の入圧を増大することができる。
最終的にこの低温は、この方法で所望の圧縮効果を減らすために圧縮機２及び４内の圧縮物を冷却するために利用することができる。
この工程はまた幾つかの点において、既知の解決方法に基づいて、例えば種々の膨張工程の間のガスを加熱し、冷却し、または圧縮することにより変形することができ、より低い最終温度、より大きい出力、その他の目的を達成できる。
二酸化炭素、特に純度の高いものは、本発明に適用分野の将来においておそらく化学工業の重要な原材料となるであろう。The invention relates to a kind of combustion and exhaust gas filtration plant combination corresponding to the part of claim 1.
Such plants are known and have in fact sufficient performance. Filtration can be very sophisticated and requires little space in this type of plant, which is important in modifying the plant being used. All process steps for this have been concentrated on the filtration process itself. However, it has been found that such a system can be further enhanced by better matching the combustor with the expansion gas filtration plant.
It is therefore an object of the present invention to further improve the filtering effect and space requirements for a combination of combustion and exhaust gas filtration plants.
According to the present invention, the combustion chamber in a combination of a combustion and exhaust gas filtration plant of the type described above is first connected to a device for supplying combustion air with 100% oxygen gas, and the separation device is connected to a final expansion step. This is achieved by connecting a small amount of non-condensable gas which has subsequently accumulated in the separation unit to a vacuum pump or the like for processing by pumping.
In fact, the combustion air contains 4 parts of nitrogen, 1 part of oxygen, and small amounts of other substances. Combustion requires a sufficient amount of oxygen, whereas nitrogen only interferes with combustion. Nitrogen, on the one hand, generates considerable amounts of hazardous substances during combustion, and on the other hand, the gas mass is greatly increased. Already increased oxygen to 2 parts relative to 3 parts nitrogen reduces the air required for combustion by half. Pure oxygen reduces the effectiveness of the compressor to less than 80%. If the volume of combustion air is significantly reduced, the size of the combustion chamber is basically limited. The temperature of the combustion chamber rises because the same amount of energy is released during combustion. This temperature rise can be balanced by increasing the heat storage area and increasing the heat radiation.
However, the nitrogen content will probably be reduced in the combustion chamber, and will provide the greatest advancement on the exhaust gas filtration side, since a very pure exhaust gas will be obtained. Also, when nitrogen is included, various types of nitric oxide are generated during combustion, and it is very difficult to separate them. During the combustion of pure oxygen, no nitric oxide is generated, regardless of whether high combustion temperatures are obtained. In an oxygen-rich atmosphere, water-soluble oxides N 2 and N 2 O 5 are first generated, which are relatively easy to separate.
The exhaust gas is composed of N 2 , CO 2 , H 2 O and small amounts of nitric oxide and pollutants contained during the combustion. Some of the water vapor to condense in the washing apparatus with water, NO 2 and N 2 O 5 is dissolved therein Like most contaminants, including SO 3 and CL types other substances. After the scrubber, N 2 , CO 2 and small amounts of material are not water-soluble and are condensed at a temperature just behind the scrubber. The more oxygen in the combustion air, the lower the amount of nitrogen in the exhaust gas immediately in front of the expansion chamber. Of course, the amount of nitric oxide and other contaminants can be reduced as a complement by adding another chemical to the wash water.
In the expansion device, the temperature drops to a level determined by the incoming gas temperature and the pressure drop. If the final temperature is below -50 ° C, the pollutants in the exhaust gas condense with the water vapor in the gas. When the temperature drops below -120 ° C, all of the carbon dioxide also condenses. If the pressure drop in the expansion chamber occurs in one step, the frozen snow and carbon dioxide snow will contain contaminants. Therefore, it is convenient to perform the expansion in two steps, the step of condensing snow and pollutants and the step of condensing pure carbon dioxide.
With this device, all pollutants in water, carbon dioxide and exhaust gas are eliminated as far as possible. Only the contained nitrogen and inert gas remain. If only oxygen were used, almost all of the gas would be converted to condensate, and the condensate would be continuously delivered and the separation chamber would be kept closed to the outside atmosphere to achieve the final The pressure can be kept close to 0 bar. This low pressure increases the pressure drop in the expansion chamber or the last one of the expansion chambers and greatly increases its efficiency. In addition, the efficiency is improved when the oxygen content is 100% or less, but does not reach the limit. To maintain this low pressure, a vacuum pump is used to continuously draw residual gas from the separator.
If the temperature before the first expansion unit is low, the temperature after the expansion device drops. By recycling the carbon dioxide snow to the scrubber, on the one hand better cooling is obtained before expansion, and on the other hand a considerably larger gas flow is obtained through the expander. In linear thermodynamic conditions, the original idea of a gas turbine system requires a supply of mechanical energy and the outlet temperature is lower than the inlet temperature. However, the process is changed by recycling the carbon dioxide condensed in the manner described above and achieving a balance in the system with this device. That is, expansion can generate as much energy as compression requires. By recycling more carbon dioxide, the expansion device generates more mechanical energy than the compressor requires. In this way, thermal energy can be converted to mechanical energy. By recycling a large amount of condensed carbon dioxide, maximum conversion can be achieved, the heat of evaporation being related to the energy supplied during combustion or to the system. In an embodiment, it should also be maintained that the temperature of the expansion device is higher than 0 ° C. Further, it is possible to supply heat energy from the outside in the form of water having a temperature higher than 0 ° C., for example, to the expansion chamber. This energy is then converted to mechanical energy.
As an example, the pressure can be increased by heating the gas with a compressor or a heat exchanger between expansion steps. Also, limiting the amount of nitrogen in the exhaust gas can limit the amount of gas to be compressed.
By cooling the gas during the expansion step, the cold gas generated after expansion can simply result in a lower final temperature or a lower initial pressure at the final temperature. Therefore, the compression effect can be reduced.
The simplest way to limit the amount of nitrogen in the incoming combustion air is to supply the required oxygen from an oxygen gas cylinder. For larger plants, for example, the use of a gas separation membrane is more economical. The oxygen generated therefrom is used in the combustion plant, while the pressurized nitrogen can drive the generator or accumulate pressurized for another use. Membrane technology and other separation methods are showing rapid development, and methods for obtaining somewhat pure oxygen, such as producing oxygen from water, are important.
Exhaust gases from plants of the above type can be recycled to the combustion chamber by a compressor during startup. The exhaust gas eliminates all environmental impact substances and is probably cleaner than the incoming combustion air.
The electrical energy required to generate oxygen and the compressors and pumps required are each used in plants equipped with the above-described devices. Low temperatures in plant operation can be used for other processes that require low temperatures.
The plant according to the invention can be modified by various methods used in combination with a thermal or power plant, and the combustion engine can be developed with this method with high efficiency and does not even contain carbon dioxide. Pure exhaust gas.
The invention will be described in more detail below with reference to the accompanying drawings, which show, schematically, by way of example of a combination of a combustion and exhaust gas filtration plant according to the invention.
The figure shows a compressor 2 driven by a motor 1 and connected to an oxygen / nitrogen separation membrane 3, the oxygen side of which is further connected to a combustion chamber 5 via a compressor 4. A combustion supply line 6 having, for example, an oil burner 7 is led into the chamber 5. In addition, substances including environmentally harmful substances may be supplied into the combustion chamber 5 for burning in the combustion chamber 5 (not shown, but in a suitable manner). Perhaps also a cylinder 8 containing oxygen can be connected to the combustion chamber 5 to increase the oxygen content if necessary.
Exhaust gas leaves the combustion chamber 5 via a line 9 connected to a boiler / cooler 10 which reduces the exhaust gas temperature shortly before being supplied to the scrubber 12 for cleaning and further pressurized cooling. Part of the water vapor in the exhaust gas condenses here. The condensate is used with the wash water in the scrubber to treat contaminants that are in particulate, water-soluble form, and are subsequently derived from the pressurized scrubber in a known manner. Exhaust gas containing the remaining contaminants is fed from the scrubber via line 13 to a first expander 14 of the rotary screw type, for example, which is suitable for driving a
The cold carbon dioxide in line 24 can also be used for re-cooling for input to a second or additional expander of the rotating screw type, which can be located. Similarly, a compressor can be installed, so that the input pressure of the second expander and additional expanders that can be arranged can be increased.
Finally, this low temperature can be used to cool the compact in compressors 2 and 4 in this way to reduce the desired compression effect.
This step can also be deformed in some respects based on known solutions, for example by heating, cooling or compressing the gas during the various expansion steps, lower final temperatures, Greater output and other goals can be achieved.
Carbon dioxide, especially of high purity, will likely be an important raw material for the chemical industry in the future of the field of application for the present invention.
Claims (2)
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE9202155A SE9202155L (en) | 1992-07-13 | 1992-07-13 | COMBINED COMBUSTION COMBUSTION AND EXHAUST WAS |
| SE9202155-9 | 1992-07-13 | ||
| PCT/SE1993/000626 WO1994001724A1 (en) | 1992-07-13 | 1993-07-13 | Combined combustion and exhaust gas cleansing plant |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH07509049A JPH07509049A (en) | 1995-10-05 |
| JP3548573B2 true JP3548573B2 (en) | 2004-07-28 |
Family
ID=20386774
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP50324094A Expired - Fee Related JP3548573B2 (en) | 1992-07-13 | 1993-07-13 | Combined plant with combustion and exhaust gas filter |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US5590519A (en) |
| EP (1) | EP0682765B1 (en) |
| JP (1) | JP3548573B2 (en) |
| DE (1) | DE69307348T2 (en) |
| SE (1) | SE9202155L (en) |
| WO (1) | WO1994001724A1 (en) |
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| WO2001075277A1 (en) * | 2000-03-31 | 2001-10-11 | Northern Research And Engineering Corporation | Solid-fueled power generation system with carbon dioxide sequestration and method therefor |
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| US6935251B2 (en) * | 2002-02-15 | 2005-08-30 | American Air Liquide, Inc. | Steam-generating combustion system and method for emission control using oxygen enhancement |
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| US7416716B2 (en) * | 2005-11-28 | 2008-08-26 | Air Products And Chemicals, Inc. | Purification of carbon dioxide |
| SE531872C2 (en) * | 2006-01-24 | 2009-09-01 | Bengt H Nilsson Med Ultirec Fa | Procedure for incremental energy conversion |
| US7861511B2 (en) * | 2007-10-30 | 2011-01-04 | General Electric Company | System for recirculating the exhaust of a turbomachine |
| US8056318B2 (en) * | 2007-11-08 | 2011-11-15 | General Electric Company | System for reducing the sulfur oxides emissions generated by a turbomachine |
| US20100018216A1 (en) * | 2008-03-17 | 2010-01-28 | Fassbender Alexander G | Carbon capture compliant polygeneration |
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| US8596075B2 (en) * | 2009-02-26 | 2013-12-03 | Palmer Labs, Llc | System and method for high efficiency power generation using a carbon dioxide circulating working fluid |
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| US20120067054A1 (en) * | 2010-09-21 | 2012-03-22 | Palmer Labs, Llc | High efficiency power production methods, assemblies, and systems |
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| US20130125580A1 (en) * | 2011-11-22 | 2013-05-23 | General Electric Company | Expander and method for co2 separation |
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| DE3924908A1 (en) * | 1989-07-27 | 1991-01-31 | Siemens Ag | Freezing dried carbon di:oxide from fossil fuel combustion - for sinking as dry ice into deep sea to counter greenhouse effect |
-
1992
- 1992-07-13 SE SE9202155A patent/SE9202155L/en not_active IP Right Cessation
-
1993
- 1993-07-13 WO PCT/SE1993/000626 patent/WO1994001724A1/en not_active Ceased
- 1993-07-13 US US08/362,596 patent/US5590519A/en not_active Expired - Fee Related
- 1993-07-13 DE DE69307348T patent/DE69307348T2/en not_active Expired - Fee Related
- 1993-07-13 JP JP50324094A patent/JP3548573B2/en not_active Expired - Fee Related
- 1993-07-13 EP EP93916364A patent/EP0682765B1/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| SE469668B (en) | 1993-08-16 |
| SE9202155D0 (en) | 1992-07-13 |
| EP0682765A1 (en) | 1995-11-22 |
| SE9202155L (en) | 1993-08-16 |
| US5590519A (en) | 1997-01-07 |
| DE69307348T2 (en) | 1997-08-21 |
| DE69307348D1 (en) | 1997-02-20 |
| WO1994001724A1 (en) | 1994-01-20 |
| JPH07509049A (en) | 1995-10-05 |
| EP0682765B1 (en) | 1997-01-08 |
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